CN101643203A - Method for recovering and utilizing steam condensate water in production of wet phosphoric acid - Google Patents
Method for recovering and utilizing steam condensate water in production of wet phosphoric acid Download PDFInfo
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- CN101643203A CN101643203A CN200910094917A CN200910094917A CN101643203A CN 101643203 A CN101643203 A CN 101643203A CN 200910094917 A CN200910094917 A CN 200910094917A CN 200910094917 A CN200910094917 A CN 200910094917A CN 101643203 A CN101643203 A CN 101643203A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention discloses a method for recovering and utilizing steam condensate water in production of wet phosphoric acid. The method comprises: firstly introducing the steam condensate water into a vacuum evaporator to be evaporated and cooled; leading the produced steam to enter a low pressure steam pipe network; after temperature reduction, leading the condensate water into a heat exchanger tobe further cooled, and then sending into a water desalination device for purification treatment; finally, supplying the obtained soft water for a waste heat boiler of a sulphuric acid device for use.The method leads part of the steam condensate water to be directly changed into steam which is supplied to a phosphoric acid concentrating device for recycling, thus avoiding energy sources being wasted. As the temperature of the steam condensate water is effectively lowered, an ultra-filtration and reverse osmosis device can be protected, and the service life of the device is prolonged. By applying the method, the heat exchange area of the heat exchanger, the quantity of circulating cooling water, the sizes of a circulating pump, a water cooling tower, a blast blower and other accessory equipment as well as the investment are reduced, and the running cost is also reduced. The method is simple in technique, water-saving, obvious in effect of energy saving, and remarkable in economic benefit.
Description
Technical field
The invention belongs to chemical production technical field, be specifically related to a kind of in the phosphoric acid by wet process concentration process, to the method for using the steam condensate that obtains after the heating steam to recycle.
Background technology
In the Chemical Manufacture evaporating concentration process, resulting steam condensate is the water of higher quality after the use heating steam, also contains heat energy.But also there is not good method to recycle this steam condensate at present.For example, when the phosphoric acid by wet process matched with devices is built sulphur-burning sulphuric acid plant, the heat that sulfur burning produces (is superheated vapour or saturation steam by sulfuric acid apparatus waste heat boiler by-product middle pressure steam, about 3.6～4.1MPa, 240～450 ℃), behind pressure and temperature reducing (generating/cooling), obtain low-pressure steam and (be superheated vapour or saturation steam, about 0.4～0.6MPa, 120～280 ℃), supply with phosphoric acid by wet process and concentrate graphite heat exchanger heated phosphoric use in the production.In the low-pressure steam use, produce a large amount of steam condensates (being entrained with steam, so temperature is higher, is 100～115 ℃).But because there is leakage sometimes in the graphite heat exchanger tubulation, will contain acid and impurity in the steam condensate, its specific conductivity, when pH value exceeds standard, can only deliver to the phosphoric acid extraction filter and cleaning process and use as washing water.When specific conductivity, when pH value does not exceed standard, be sent to sulfuric acid apparatus desalination water station and carry out the desalination purification, obtain refining de-salted water (soft water) and use for waste heat boiler.All de-salted water devices all are provided with ion-exchange resin (cloudy bed, sun bed---mixed bed) and/or ultrafiltration and reverse osmosis membrane on purification process.The equal non-refractory of resin and film, suitable operation at a lower temperature so steam condensate need adopt interchanger to carry out the heat exchange cooling, after temperature is reduced, just can enter the de-salted water device and carry out the desalination purification.Mainly there is the problem of three aspects in above production technique: the steam condensate of (1) higher quality is taken as general water and uses; (2) heat energy that needs interchanger to shift out is many, and the recirculated cooling water requirement is big, the investment of equipment such as recycle pump, water cooling tower and working cost height; When (3) desalination purifies the soft water obtain and enters the sulfuric acid apparatus waste heat boiler, need to absorb more heat transfer again and become steam.As can be seen, in the whole process of production, the utilization of steam condensate is very unreasonable.At present, still there is not good method to overcome the problems referred to above in the prior art.
Summary of the invention
The objective of the invention is at the deficiencies in the prior art, recovering and utilizing steam condensate in a kind of Wet-process Phosphoric Acid Production is provided.
Purpose of the present invention is achieved by the following technical programs.
Recovering and utilizing steam condensate in the Wet-process Phosphoric Acid Production is characterized in that: steam condensate is introduced vacuum-evaporator evaporation, cooling earlier, and the steam of generation enters the low-pressure steam pipe network, and the water of condensation after the cooling imports further cooling in the interchanger.
Be specially: evaporate, cool off using 100～115 ℃ the steam condensate that obtains after the heating steam to send into earlier in the vacuum-evaporator in the phosphoric acid by wet process concentration process, this part steam that is evaporated directly enters the low-pressure steam pipe network, the supply phosphoric acid concentrating device recycles, evaporate water of condensation after remaining, the cooling and deliver to interchanger further after the cooling, deliver to the de-salted water device again and carry out purifying treatment, the soft water that obtains is supplied with the sulfuric acid apparatus waste heat boiler and is used.
Described vacuum-evaporator places before the interchanger, and is connected with reducing-and-cooling plant by pipeline, by reducing-and-cooling plant vacuum-evaporator is vacuumized.
Described vacuum-evaporator evaporated water is at 4.50～36.07 (t H
2O)/and h, the vacuum-evaporator evaporation area is 8.37m
2～67.12m
2, the vacuum-evaporator diameter is 3.26m～9.25m.
Further, described vacuum-evaporator evaporated water is 9.00～27.00 (t H
2O)/and h, the vacuum-evaporator evaporation area is 16.74m
2～50.24m
2, the vacuum-evaporator diameter is 4.62m～8.00m.
Vacuum-evaporator absolute pressure scope 7.0KPa～94.0KPa, preferred vacuum-evaporator absolute pressure scope 8.0KPa～20.0KPa.
Principle of work of the present invention: after the steam condensate that production process produces enters vacuum-evaporator, 100～115 ℃ the temperature that vacuum of utilizing the middle pressure steam pressure and temperature reducing to become to produce in the process of low-pressure steam and steam condensate itself have, produce explosive evaporatoin, shift out a part of heat, reduce the temperature of water of condensation; Simultaneously, the steam that is evaporated directly enters the low-pressure steam pipe network by reducing-and-cooling plant, a part of steam condensate has directly been become steam offered phosphoric acid concentrating device and recycle.Water of condensation behind the evaporative cooling is delivered to the de-salted water device again and is carried out purifying treatment after delivering to the further cooling of interchanger, and the soft water that obtains is supplied with the sulfuric acid apparatus waste heat boiler and used.
The present invention makes full use of the middle pressure steam pressure and temperature reducing to be become the temperature that the vacuum that produces in the process of low-pressure steam and steam condensate self have and carries out explosive evaporatoin, a part of steam condensate has directly been become steam, supplied with phosphoric acid concentrating device and recycle.Simultaneously, the present invention also effectively reduces the temperature of steam condensate, the inflow temperature of de-salted water device is stablized to be controlled at lower level easily, can effectively protect ultrafiltration, reverse osmosis unit.Increase a vacuum-evaporator, shift out a part of heat earlier by vacuum-evaporation, can reduce the amount of thermal energy that need shift out by interchanger, thereby reduce the size and the investment of the auxiliary facilitys such as heat interchanging area, quantity of circulating cooling water and recycle pump, water cooling tower, gas blower of interchanger, reduce working cost.Water saving of the present invention, energy-saving effect are obvious, remarkable in economical benefits.
Description of drawings
Fig. 1 utilizes process flow diagram for reclamation of condensate water in the prior art;
Fig. 2 utilizes process flow diagram for reclamation of condensate water of the present invention.
Embodiment
Below in conjunction with drawings and Examples, the present invention is further illustrated, but they all are not limitation of the invention.
Embodiment 1
As shown in Figure 2, on the basis of existing equipment, increase a vacuum-evaporator, connect after condensate draining, before the interchanger, and vacuum-evaporator is connected with reducing-and-cooling plant by Φ 1.27m pipeline, vacuum-evaporator is vacuumized by reducing-and-cooling plant.The diameter of this vacuum-evaporator is 5.66m, and evaporation area is 25.12m
2, the absolute pressure operating restraint is 9.0～14.6KPa, evaporated water 13.50 (t H
2O)/h.
Condensate temperature is 112 ℃, and through vacuum-evaporation, temperature is reduced to 80～90 ℃, and through the interchanger cooling, temperature is reduced to 39 ℃, enters the de-salted water device and purifies again.
Embodiment 2
As shown in Figure 2, on the basis of existing equipment, increase a vacuum-evaporator, connect after condensate draining, before the interchanger, and vacuum-evaporator is connected with reducing-and-cooling plant by Φ 1.80m pipeline, vacuum-evaporator is vacuumized by reducing-and-cooling plant.The diameter of this vacuum-evaporator is 8.00m, and evaporation area is 50.24m
2, the absolute pressure operating restraint is 10.0～16.0KPa, evaporated water 27.00 (t H
2O)/h.
Condensate temperature is 108 ℃, and through vacuum-evaporation, temperature is reduced to 70～80 ℃, and through the interchanger cooling, temperature is reduced to 38 ℃, enters the de-salted water device and purifies again.
Embodiment 3
As shown in Figure 2, on the basis of existing equipment, increase a vacuum-evaporator, connect after condensate draining, before the interchanger, and vacuum-evaporator is connected with reducing-and-cooling plant by Φ 1.04m pipeline, vacuum-evaporator is vacuumized by reducing-and-cooling plant.The diameter of this vacuum-evaporator is 4.62m, and evaporation area is 16.74m
2, the absolute pressure operating restraint is 8～12KPa, evaporated water 9.00 (tH
2O)/h.
Condensate temperature is 105 ℃, and through vacuum-evaporation, temperature is reduced to 85～95 ℃, and through the interchanger cooling, temperature is reduced to 40 ℃, enters the de-salted water device and purifies again.
Claims (6)
1, recovering and utilizing steam condensate in the Wet-process Phosphoric Acid Production is characterized in that: steam condensate is introduced vacuum-evaporator evaporation, cooling earlier, and the steam of generation enters the low-pressure steam pipe network, and the water of condensation after the cooling imports further cooling in the interchanger.
2, recoverying and utilizing method according to claim 1 is characterized in that: described vacuum-evaporator places before the interchanger, and is connected with reducing-and-cooling plant by pipeline, by reducing-and-cooling plant vacuum-evaporator is vacuumized.
3, recoverying and utilizing method according to claim 2 is characterized in that: described vacuum-evaporator evaporated water is 4.50～36.07 (t H
2O)/and h, the vacuum-evaporator evaporation area is 8.37m
2～67.12m
2, the vacuum-evaporator diameter is 3.26m～9.25m.
4, recoverying and utilizing method according to claim 3 is characterized in that: described vacuum-evaporator evaporated water is 9.00～27.00 (t H
2O)/and h, the vacuum-evaporator evaporation area is 16.74m
2～50.24m
2, the vacuum-evaporator diameter is 4.62m～8.00m.
5, recoverying and utilizing method according to claim 2 is characterized in that: described vacuum-evaporator absolute pressure scope 7.0KPa～94.0Kpa.
6, recoverying and utilizing method according to claim 5 is characterized in that: described vacuum-evaporator absolute pressure scope 8.0KPa～20.0KPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910094917A CN101643203A (en) | 2009-09-02 | 2009-09-02 | Method for recovering and utilizing steam condensate water in production of wet phosphoric acid |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910094917A CN101643203A (en) | 2009-09-02 | 2009-09-02 | Method for recovering and utilizing steam condensate water in production of wet phosphoric acid |
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|---|---|
| CN101643203A true CN101643203A (en) | 2010-02-10 |
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|---|---|---|---|
| CN200910094917A Pending CN101643203A (en) | 2009-09-02 | 2009-09-02 | Method for recovering and utilizing steam condensate water in production of wet phosphoric acid |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102060272A (en) * | 2010-11-07 | 2011-05-18 | 湖南新恒光科技有限公司 | Refrigeration method and technique in sulfuric acid production process |
| CN102531007A (en) * | 2010-12-26 | 2012-07-04 | 中铝国际技术发展有限公司 | Whole plant live steam condensed water heat energy recycling device of aluminum oxide production |
| CN102677077A (en) * | 2011-12-12 | 2012-09-19 | 北京星和众工设备技术股份有限公司 | Damage monitoring system for graphite heat exchanger on pickling line |
| CN103011456A (en) * | 2012-12-12 | 2013-04-03 | 贵州开磷（集团）有限责任公司 | Method for recycling condensate water in phosphoric acid concentration system |
| CN105110307A (en) * | 2015-07-29 | 2015-12-02 | 贵州开磷集团股份有限公司 | Steam condensate water heat recovery method of water desalination device combined phosphoric acid condensation device |
| CN106882777A (en) * | 2017-04-06 | 2017-06-23 | 南通三圣石墨设备科技股份有限公司 | A kind of purifying phosphoric acid concentration technology |
-
2009
- 2009-09-02 CN CN200910094917A patent/CN101643203A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102060272A (en) * | 2010-11-07 | 2011-05-18 | 湖南新恒光科技有限公司 | Refrigeration method and technique in sulfuric acid production process |
| CN102060272B (en) * | 2010-11-07 | 2012-04-25 | 湖南新恒光科技有限公司 | Refrigeration method and technique in sulfuric acid production process |
| CN102531007A (en) * | 2010-12-26 | 2012-07-04 | 中铝国际技术发展有限公司 | Whole plant live steam condensed water heat energy recycling device of aluminum oxide production |
| CN102677077A (en) * | 2011-12-12 | 2012-09-19 | 北京星和众工设备技术股份有限公司 | Damage monitoring system for graphite heat exchanger on pickling line |
| CN103011456A (en) * | 2012-12-12 | 2013-04-03 | 贵州开磷（集团）有限责任公司 | Method for recycling condensate water in phosphoric acid concentration system |
| CN105110307A (en) * | 2015-07-29 | 2015-12-02 | 贵州开磷集团股份有限公司 | Steam condensate water heat recovery method of water desalination device combined phosphoric acid condensation device |
| CN106882777A (en) * | 2017-04-06 | 2017-06-23 | 南通三圣石墨设备科技股份有限公司 | A kind of purifying phosphoric acid concentration technology |
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Open date: 20100210 |